JP2018124019A - Heat exchanger and heat exchange system - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a heat exchanger and a heat exchange system, capable of optimizing performance related to heat exchange for each portion, to suppress enlargement of a device.SOLUTION: A heat exchanger includes: a first shell 3 storing a first heating line 2; a second shell storing a second heating line 4 positioned on a downstream side of the first heating line 2; and an intermediate shell 6 positioned between the first shell 3 and the second shell 5, and configured to circulate heated fluid L to an internal space, wherein at least any one of a flow passage cross sectional area for the heated fluid L, a contact area with heat medium A per volume of the heated fluid L and a capacity of the heat medium A per volume of the heated fluid L, of the first shell 3 is made larger than that of the second shell 5.SELECTED DRAWING: Figure 1

Description

  The present invention relates to a heat exchanger and a heat exchange system for heating a fluid such as liquefied natural gas.

  In general, when liquefied natural gas (LNG) is used as a fuel, LNG stored at a low temperature is heated and vaporized, and in some cases, the vaporized natural gas (NG) is overheated to a required temperature. It needs to be warmed. At this time, as a device for vaporizing and overheating LNG, for example, a type of heat exchanger called a shell and tube type is used (for example, see Patent Document 1 below).

  In this type of heat exchanger, a tube (tube) as a flow path of LNG is accommodated in the shell, a heat medium is circulated in the shell, and the LNG flowing in the tube and the periphery of the tube LNG is heated by exchanging heat with the flowing heat medium.

  In the following, among the series of steps of heating the heated fluid such as LNG using a heat exchanger, the step of vaporizing the heated fluid in a liquid state is referred to as “vaporization”. Further, the process of increasing the temperature by applying heat is specifically referred to as “overheating”.

Special table 2008-518187 gazette

  In the heat exchanger as described above, in order to satisfy the required performance, specifications such as the diameter and length of the tubes, the number of tubes, the interval between the tubes, and the size of the shell are appropriately determined in the design stage. Here, in the case of a conventional shell-and-tube heat exchanger, each of the pipes forming the LNG flow path is composed of a single pipe from the inlet to the outlet. That is, the diameter and number of each pipe, the interval between the pipes, and the like are the same over the entire flow path from the inlet to the outlet of the shell.

  On the other hand, in the heat exchanger used for LNG vaporization, the heat exchange amount per unit length in the upstream flow path and the heat exchange amount per unit length in the downstream flow path are greatly different. On the upstream side, the amount of heat exchange is large in order to take heat of vaporization from the heat medium in the process of vaporizing LNG, which is liquid, to NG, but on the downstream side, a process of superheating vaporized NG is performed, so the upstream side The amount of heat exchange is small compared to

  However, as described above, the flow path configuration according to the diameter and arrangement of the tubes is the same between the upstream side and the downstream side, and the performance related to heat exchange in design does not differ between the upstream side and the downstream side. Therefore, when the diameter and arrangement of the pipes are determined so as to prevent the heat medium from freezing in consideration of the amount of heat exchange on the upstream side, the design performance with respect to the actual heat exchange amount is excessive on the downstream side. Become. However, if the pipe is designed to match the amount of heat exchange on the downstream side, the design performance will be insufficient for the amount of heat exchange required on the upstream side. The entire design must be designed according to the amount of heat exchange. Thus, in the conventional shell and tube type heat exchanger, the performance related to the heat exchange is partially excessive with respect to the required heat exchange amount. Had happened. Increasing the size of the apparatus requires an increase in the size of the installation base, leading to an increase in construction costs, and may limit transportation in terms of limited vehicles that can be loaded.

  In view of such circumstances, the present invention intends to provide a heat exchanger and a heat exchange system that can optimize the performance related to heat exchange for each part and suppress the enlargement of the apparatus.

  In the present invention, a first heating line for circulating a fluid to be heated is accommodated therein, and a first shell configured to supply a heat medium around the first heating line and the first heating line are passed. A second heating line for circulating a fluid to be heated is accommodated therein, a second shell configured to supply a heat medium around the second heating line, and between the first shell and the second shell And an intermediate shell configured to circulate a heated fluid in a space provided therein, and a flow path cross-sectional area of the heated fluid in the first shell, and a heat medium per volume of the heated fluid At least one of the contact area and the capacity of the heat medium per volume of the fluid to be heated is applied to the heat exchanger configured to be larger than the second shell.

  In concretely implementing the heat exchanger of the present invention, the first heating line is configured as a plurality of tubes, the second heating line is configured as one or more tubes, and the first heating line is configured. The number of tubes can be made larger than the number of tubes constituting the second heating line.

  In concrete implementation of the heat exchanger of the present invention, the first heating line and the second heating line are each configured as a plurality of tubes, and the interval between the tubes constituting the first heating line is set to the first. The area of the cross section perpendicular to the pipe of the first shell can be set larger than the area of the cross section perpendicular to the pipe of the second shell.

  The heat exchanger of this invention can be comprised so that the to-be-heated fluid introduced into the said 1st heating line from the lower part of the said 1st shell may be extracted above the said 2nd heating line through the said intermediate shell.

  Further, the present invention provides the heat exchanger according to claim 1, wherein the heat exchanger includes at least one of a temperature sensor that detects a temperature of the fluid to be heated and a pressure sensor that detects a pressure of the fluid to be heated. This is related to the heat exchange system used.

  In the heat exchange system of the present invention, it is preferable that the temperature sensor or the pressure sensor is provided in the intermediate shell.

  According to the heat exchanger and the heat exchange system of the present invention, it is possible to optimize the performance related to heat exchange for each part and to achieve an excellent effect of suppressing the increase in size of the apparatus.

It is a front sectional view explaining the form of the heat exchanger by the 1st example of the present invention. It is a front sectional view explaining the form of the heat exchanger by 2nd Example of this invention. It is a front sectional view explaining the form of the heat exchanger by 3rd Example of this invention. It is a front sectional view explaining the form of the heat exchanger by 4th Example of this invention. It is a block diagram explaining an example of the heat exchange system by implementation of this invention.

  Embodiments of the present invention will be described below with reference to the accompanying drawings.

  FIG. 1 shows a heat exchanger according to a first embodiment of the present invention. The heat exchanger 1 of the first embodiment is of a type classified as a shell and tube type, but a shell containing a pipe is divided into two stages, an upstream side and a downstream side, and an intermediate shell is formed between them. It is characterized in that it is possible to change the flow path configuration using a pipe between the two-stage shells.

  As shown in FIG. 1, the heat exchanger 1 is heated in the same manner as the first shell 3 on the upstream side containing a plurality of pipes 2 as first heating lines through which a heated fluid L such as LNG flows. And a second shell 5 containing a plurality of tubes 4 as second heating lines through which the fluid L flows. The first shell 3 and the second shell 5 are connected by an intermediate shell 6. The first shell 3 and the second shell 5 are configured so that the heat medium A is introduced into the inside thereof, and the heat medium A introduced into the first shell 3 and the second shell 5 is formed by the pipes 2 and 4. The fluid to be heated is brought into contact with the fluid to be heated L via the pipes 2 and 4, and heat exchange with the fluid to be heated L is performed. The second shell 5 is disposed above the first shell 3 via the intermediate shell 6, and the upstream and downstream pipes 2, 4 are vertically oriented inside the first shell 3 or the second shell 5, respectively. It is arranged in the direction along.

  The first shell 3 is a hollow member having a cylindrical shape as a whole, and is formed by covering the bottom surface of the side surface 3a forming a cylindrical surface with the bottom plate 3b and the top surface with the top plate 3c. A heat medium inlet 3d for introducing the heat medium A into the first shell 3 and a heat medium outlet 3e for deriving the heat medium A from the first shell 3 are provided at appropriate positions on the side surface 3a. . In the example shown here, the heat medium inlet 3d is provided at one location near the upper end of the side surface 3a, and the heat medium outlet 3e is disposed at one location near the lower end on the opposite side of the heat medium inlet 3d with respect to the central axis of the side surface 3a. Is arranged.

  The tube 2 constituting the first heating line extends from the bottom plate 3b to the top plate 3c, and the bottom plate 3b and the top plate 3c are respectively penetrated through the end portions of the tubes 2 provided inside the first shell 3. Yes. Thus, the space inside the tube 2 through which the fluid L to be heated flows and the space inside the first shell 3 through which the heat medium A flows and outside the tube 2 are isolated from each other.

  Inside the first shell 3, two baffle plates 7 a and 7 b are provided so as to form a surface orthogonal to the tube 2. Among these, the baffle plate 7a located on the upper side is divided so as to cross the space in the first shell 3 below the heat medium inlet 3d. The baffle plate 7a is formed on the side surface 3a on the heat medium outlet 3e side. The vicinity of the inner wall is not closed, and an opening exists between the inner wall and the inner wall. Further, the baffle plate 7b located on the lower side forms a surface along the horizontal direction above the heat medium outlet 3e to divide the space in the first shell 3, but the baffle plate 7b on the side 3a on the heat medium inlet 3d side is separated. There is an opening between the inner wall. These baffle plates 7a and 7b are penetrated by the pipe 2 at the locations where they intersect with the pipes 2, and do not hinder the flow path of the heated fluid L inside the pipe 2. That is, the baffle plates 7a and 7b are installed in a space in the first shell 3 that is isolated from the space in the tube 2.

  The heating medium A introduced into the first shell 3 from the heating medium inlet 3d first flows in the vicinity of the upper plate 3c in the first shell 3 along the horizontal direction, and the inner wall of the side surface 3a opposite to the heating medium inlet 3d. It flows downward while bypassing the baffle plate 7a in the vicinity. Furthermore, after flowing between the baffle plate 7a and the baffle plate 7b toward the heat medium inlet 3d along the horizontal direction, the flow is directed downward while bypassing the baffle plate 7b, and flows around the bottom plate 3b along the horizontal direction. The heat medium outlet 3e is reached. In this way, by arranging the baffle plates 7a and 7b in the first shell 3 alternately with respect to the flow path of the heat medium A, the heat medium A introduced from the heat medium inlet 3d is caused to meander around the pipe 2. However, it leads to the heat medium outlet 3e. By meandering the flow of the heat medium A in this way, the chance of the heat medium A contacting the heated fluid L via the pipe 2 is increased, and the heat exchange efficiency is improved. Here, the case where two baffle plates 7a and 7b are provided in the first shell 3 as baffle plates is illustrated, but the dimensions of the first shell 3, the arrangement of the heat medium inlet 3d, the heat medium outlet 3e, etc. In addition, the number of baffle plates can be increased or decreased. When increasing the number of baffle plates, it is advantageous in terms of heat exchange efficiency if the heat medium A meanders by arranging a plurality of baffle plates alternately like the baffle plates 7a and 7b described above. .

  The second shell 5 has a configuration substantially similar to that of the first shell 3 and is a hollow member having a cylindrical shape as a whole. The bottom surface of the side surface 5a that forms a cylindrical surface is covered with the bottom plate 5b, and the top surface is covered with the top plate 5c, and the tubes 4 constituting the second heating line extend from the bottom plate 5b to the top plate 5c. The bottom plate 5b and the top plate 5c penetrate through the end of the tube 4, and the space inside the tube 4 and the space inside the second shell 5 and outside the tube 4 are isolated from each other. A heat medium inlet 5d is provided at one location near the upper end of the side surface 5a, and a heat medium outlet 5e is provided at one location near the lower end on the opposite side of the central axis of the side surface 5a from the heat medium inlet 5d. The heat medium A is circulated in a space inside and outside the tube 4. In the example shown here, the second shell 5 is not provided with a configuration corresponding to the baffle plates 7a and 7b in the first shell 3, but depending on the size of the second shell 5 and the required heat exchange amount. May be provided with baffle plates similar to the baffle plates 7a and 7b as appropriate.

  In the case of the first embodiment, between the first shell 3 and the second shell 5, the numbers of the tubes 2 and 4 accommodated therein are different from each other. The number of tubes 2 constituting the line is set to be larger than the number of tubes 4 constituting the second heating line in the second shell 5. Accordingly, the diameter of the first shell 3 is set larger than the diameter of the second shell 5. FIG. 1 is a schematic diagram conceptually illustrating the configuration of the heat exchanger 1, and the diameters and number of the tubes 2 and 4 shown in FIG. 1 do not necessarily reflect the actual conditions. The same applies to FIGS. 2 to 5 below.

  In the first embodiment, the material, diameter, and thickness of each tube 2 are the same as the material, diameter, and thickness of each tube 4, and therefore, it relates to heat exchange per unit length of one tube. The performance is equal between tube 2 and tube 4. However, since the number of the tubes 2 is larger than the number of the tubes 4, the flow path cross-sectional area of the entire first heating line is larger than the flow path cross-sectional area of the entire second heating line. Therefore, if the heated fluid L is circulated at the same speed and the same density, the amount of the heated fluid L flowing per unit length of the entire pipe 2 constituting the first heating line is the same as that of the second heating line. The amount is larger than the amount of the heated fluid L that flows per unit length of the entire tube 4 to be configured. Further, if the heated fluid L is circulated in the same amount, the flow rate of the heated fluid L flowing through the tube 2 is slower than the flow rate of the heated fluid L flowing through the tube 4.

  The intermediate shell 6 is a hollow member installed between the lower first shell 3 and the upper second shell 5. The side surface 6a of the intermediate shell 6 forms a conical surface of a truncated cone as a whole. The lower diameter of the conical surface is the diameter of the upper plate 3c of the first shell 3, and the upper diameter is the second shell. 5 is equal to the diameter of the bottom plate 5b. The lower end and upper end of the side surface 6a are circumferentially welded to the upper end of the side surface 3a of the first shell 3 and the lower end of the side surface 5a of the second shell 5, respectively, and the side surface 6a of the intermediate shell 6 and the upper plate of the first shell 3 A frustoconical space is formed by 3c and the bottom plate 5b of the second shell 5. This space communicates with the space inside the tube 2 forming the first heating line and the space inside the tube 4 forming the second heating line, the space outside the tube 2 and inside the first shell 3, and The space outside the tube 4 and inside the second shell 5 is isolated from the top plate 3c of the first shell 3 and the bottom plate 5b of the second shell 5, respectively. Thus, the intermediate shell 6 forms a flow path of the heated fluid L that communicates between the first heating line constituted by the pipe 2 and the second heating line constituted by the pipe 4.

  A front chamber 8 is provided below the first shell 3 so as to cover the lower side of the bottom plate 3 b, and the heated fluid L passes from the heated fluid inlet 8 a provided in the front chamber 8 to the inside of the front chamber 8. It is supplied to the space and introduced from here into the pipe 2 which is the first heating line. In addition, a rear chamber 9 is provided above the second shell 5 so as to cover the upper side of the upper plate 5 c, and the heated fluid L flowing through the pipe 4 serving as the second heating line passes through the rear chamber 9. After being guided to the internal space, it flows out from the heated fluid outlet 9a provided in the rear chamber 9 to the downstream.

  Thus, in the heat exchanger 1 of the first embodiment, the heated fluid L is introduced into the front chamber 8 from the heated fluid inlet 8a at the lower portion of the heat exchanger 1 and flows into the pipe 2 from below, so that the first After exchanging heat with the heat medium A in the shell 3, the heat medium A is extracted into the upper intermediate shell 6, and further flows into the lower part of the pipe 4 from the intermediate shell 6 to exchange heat with the heat medium A in the second shell 5. It is extracted from the rear chamber 9 through an upper heated fluid outlet 9a.

  At this time, as described above, the number of the tubes 2 constituting the first heating line is larger than the number of the tubes 4 constituting the second heating line. Therefore, the contact area with the heating medium A per volume of the fluid L to be heated is larger in the tube 2 than in the tube 4. Further, since the total number of the flow path cross-sectional areas of the heated fluid L is larger than that of the pipe 4 because the number of the pipes 2 is larger, the flow velocity of the heated fluid L is slower. For this reason, since the fluid L to be heated is heated while slowly flowing through the pipe 2, the amount of heat exchange per unit length increases. Thereby, the performance concerning the heat exchange in the first shell 3 is higher than that of the second shell 5.

  As described above, in the first shell 3, the heated fluid L that flows in as a low-temperature liquid is mainly vaporized, and a large amount of heat of vaporization is deprived from the heat medium A, so that a large amount of heat exchange is required. If the contact area between the heated fluid L and the heating medium A is large and the flow velocity of the heated fluid L is small, much heat can be transferred from the heating medium A to the heated fluid L. The heated fluid L is vaporized efficiently in the one shell 3.

  At this time, in the first shell 3, the interval between the tubes 2 is set wider than the interval between the tubes 4. Moreover, since the area of the cross section orthogonal to the pipe 2 of the first shell 3 is larger than the area of the cross section orthogonal to the pipe 4 of the second shell 5, the capacity of the heating medium A in the first shell 3 is It is ensured sufficiently large with respect to the volume of the heated fluid L flowing through the pipe 2. Accordingly, it is possible to prevent a situation in which the heat medium A, which has been deprived of a large amount of heat by the vaporization of the heated fluid L, is frozen.

  On the other hand, in the second shell 5, the heated fluid L vaporized in the first shell 3 circulates, and only the overheating of the heated fluid L is performed here, so that the required heat exchange efficiency is small. . Therefore, even if the contact area of the fluid L to be heated with the heat medium A is smaller than that of the first shell 3 and the flow velocity is high, there is no performance problem.

  As described above, in the heat exchanger 1 of the first embodiment, the upstream shell of the heat exchanger 1 is divided by dividing the shell, which has conventionally been one stage, into two stages of the first shell 3 and the second shell 5. The flow path configuration can be changed between the downstream side and the performance related to heat exchange can be made different. Therefore, the first shell 3 and the second shell 5 are each designed according to the performance required for heat exchange, and the performance of each part of the heat exchanger 1 is optimized to match the performance required for each part. It is possible. In the conventional heat exchanger, the downstream flow path, where the performance related to heat exchange is excessive, can be configured to match the performance that is originally required, and as a result, the flow path for surplus performance The structure which concerns on can be reduced, and the enlargement of an apparatus can be suppressed. At this time, since the intermediate shell 6 is interposed between the first shell 3 and the second shell 5 as a flow path of the fluid L to be heated, a pipe is formed between the first shell 3 and the second shell 5. Even if the flow path configurations of 2 and 4 are different, there is no inconvenience regarding the flow of the heated fluid L.

  At this time, the heated fluid L that has passed through each pipe 2 is extracted into the intermediate shell 6 and then introduced into the downstream pipe 4. 4 will flow in. Therefore, even if there is a variation between the tubes 2 regarding the temperature of the heated fluid L at the outlet of the tube 2, the heated fluid L extracted from each tube 2 in the intermediate shell 6 is mixed as a result. The effect that the temperature of the heated fluid L drawn out from above the tube 4 is homogenized can also be expected.

  Here, FIG. 1 exemplifies a case where a structure or the like is not particularly provided inside the intermediate shell 6. For example, a rectifying plate that induces the flow of the heated fluid L or an intermediate shell 6 is provided in this portion. A structural material or the like for securing the strength may be separately provided.

  Moreover, about the pipe | tubes 2 and 4, by adjusting each length suitably, the flow-path length which contacts the heat carrier A is adjusted, Therefore The heat exchange amount in each of the 1st shell 3 and the 2nd shell 5 is adjusted. Can be adjusted. That is, the length of the pipe 2 is a flow path length capable of appropriately performing vaporization of the heated fluid L, and the length of the pipe 4 is a flow path length capable of overheating the vaporized heated fluid L to a necessary temperature. Each may be set as appropriate in the design stage.

  In the first shell 3 and the second shell 5, as described above, the heating medium A flows from the heating medium inlets 3d and 5d provided near the upper end toward the heating medium outlets 3e and 5e provided near the lower end, respectively. It has become. On the other hand, since the heated fluid L flowing through the pipe 2 and the pipe 4 flows from the bottom to the top, the flow of the heated fluid L and the flow of the heating medium A form a counterflow that faces each other vertically. For the heating medium A, the temperature gradually decreases as heat is gradually removed from above the first shell 3 or the second shell 5, and for the heated fluid L, the temperature increases from below to above. Therefore, heat exchange with high efficiency can be achieved.

  The structure in which the shell is divided in this manner has advantages in terms of strength and durability. In the conventional heat exchanger, each pipe constituting the flow path is a single long pipe from the upstream to the downstream, so that the rigidity is reduced, and there is a tendency that torsion, vibration, deformation due to them tend to occur. It was. In the case of the heat exchanger 1 of the first embodiment, the pipe 2 and the pipe 4 constituting the first heating line and the second heating line are divided into respective shells (first shell 3, second shell). Since it is equal to the length of the shell 5), the total length is significantly shorter than that of a conventional heat exchanger using a single-stage shell. Therefore, it is easy to maintain the rigidity of each of the tubes 2 and 4, and problems such as vibration and deformation can be easily avoided.

  Here, in the first embodiment described above, a two-stage heat exchange in which one intermediate shell 6 is provided between two shells (first shell 3 and second shell 5) containing the tubes 2 and 4. Although the container 1 is illustrated, the configuration of the present invention is not limited to this. For example, a total of three shells containing tubes can be provided, and a three-stage heat exchanger having two intermediate shells between the three shells can be provided. It doesn't matter. In addition, the number of shells per heat exchanger can be changed as appropriate. The same applies to the second to fourth embodiments described later.

  As described above, in the heat exchanger 1 of the first embodiment, the first shell 3 that houses the first heating line 2 and the second heating line 4 that is located downstream of the first heating line 2 are provided. A second shell accommodated, and an intermediate shell 6 positioned between the first shell 3 and the second shell 5 and configured to circulate the heated fluid L in a space provided therein, At least one of the flow path cross-sectional area of the heated fluid L in one shell 3, the contact area with the heating medium A per volume of the heated fluid L, or the capacity of the heating medium A per volume of the heated fluid L is Since it is configured to be larger than the second shell 5, the performance relating to heat exchange in the first shell 3 can be made different from that of the second shell 5.

  In the heat exchanger 1 of the present invention, the first heating line 2 is configured as a plurality of tubes 2, the second heating line 4 is configured as one or more tubes 4, and the number of tubes 2 is the number of tubes 4. Since the number is larger than the number, the contact area between the flow path cross-sectional area of the heated fluid L in the first shell 3 and the heating medium A per volume of the heated fluid L is made larger than that of the second shell 5 with a simple configuration. be able to.

  In the heat exchanger 1 of the present invention, the interval between the tubes 2 is set wider than the interval between the tubes 4, and the cross-sectional area orthogonal to the tube of the first shell is orthogonal to the tube of the second shell. Therefore, the capacity of the heating medium A per volume of the heated fluid L in the first shell 3 can be made larger than that of the second shell 5 with a simple configuration.

  In the heat exchanger 1 of the present invention, the heated fluid L introduced into the first heating line 2 from the lower part of the first shell 3 is extracted to the upper side of the second heating line 4 through the intermediate shell 6. Since it is comprised, about the type heat exchanger 1 which draws out the to-be-heated fluid L introduced from the downward direction, the performance which concerns on heat exchange can be optimized for every part.

  Therefore, according to the heat exchanger of the first embodiment, the performance related to heat exchange can be optimized for each portion, and the increase in size of the apparatus can be suppressed.

  FIG. 2 shows a heat exchanger according to a second embodiment of the present invention. The basic configuration is the same as that of the heat exchanger 1 (see FIG. 1) of the first embodiment, but in the case of the heat exchanger 21 of the second embodiment, the upstream first shell 23 and the downstream side By optimizing the performance related to heat exchange, the diameter and arrangement of the second shell 25 are different from the number of the pipes 22 and 24 instead of the number of the pipes 22 and 24.

  Specifically, the diameter of the pipe 22 constituting the upstream first heating line is larger than that of the pipe 24 constituting the downstream second heating line. In this way, the contact area of the pipe 22 with the heating medium A per volume of the heated fluid L is smaller than that of the pipe 24, but the flow velocity of the heated fluid L in the pipe 22 is smaller than the flow velocity in the pipe 24. If the flow velocity is sufficiently small, the amount of heat exchange per unit length can be increased. Therefore, the performance related to the heat exchange required in the upstream first shell 23 where the heated fluid L is vaporized can be obtained. It can be secured sufficiently. At this time, the space between the tubes 22 constituting the first heating line is widened, and the cross-sectional area of the first shell 23 is increased, so that a sufficient amount of the heat medium A for heat exchange is supplied to the tubes 22. It is possible to prevent the heat medium A from freezing. On the other hand, the second shell 25 that superheats the vaporized heated fluid L does not require the same performance as the first shell 23 in terms of heat exchange, and there is no possibility that the heating medium A freezes. There is no particular problem even if the flow rate of the heated fluid L is increased, the interval between the tubes 24 is reduced, and the cross-sectional area of the second shell 25 is reduced.

  Since other configurations and operational effects are the same as those of the heat exchanger of the first embodiment, the description thereof will be omitted. It can optimize and suppress the enlargement of the device.

  FIG. 3 shows a heat exchanger according to a third embodiment of the present invention. The basic configuration is the same as that of the heat exchanger 1 (see FIG. 1) and the heat exchanger 21 (see FIG. 2) of the first and second embodiments, but of the heat exchanger 31 of the third embodiment. In this case, the number of the tubes 32 of the upstream first shell 33 is made larger than the number of the tubes 34 of the downstream second shell 35, and the diameter of each tube 32 is made smaller than the diameter of each tube 34. Thereby, in the pipe | tube 32 which comprises a 1st heating line, the contact area with the heat medium A per volume of the to-be-heated fluid L is larger than the pipe | tube 34 which comprises a 2nd heating line. The total of the cross-sectional areas of the heated fluid L in the pipe 32 is equal to the total of the cross-sectional areas of the pipe 34.

  In this way, the flow rate of the heated fluid L is not significantly different between the pipe 32 and the pipe 34 (however, since the vaporized heated fluid L flows through the pipe 34, the liquid flow in the pipe 32). However, the pipe 32 has a large contact area with the heat medium A, so that high heat exchange efficiency is ensured.

  Here, in the third embodiment, the contact area between the heated fluid L and the heating medium A in the first heating line 32 is increased by installing a larger number of the pipes 32 than the pipes 34. Is not limited to the change in the number of tubes, and can be achieved by, for example, changing the shape of the tube 32. For example, if the tube 32 is configured as a flat tube and the tube 34 is configured as a circular tube, the heated fluid L and the heating medium A in the tube 32 even if the total flow cross-sectional area is equal between the tubes 32 and 34. The contact area becomes larger than that of the tube 34.

  Since other configurations and operational effects are the same as those of the heat exchanger of the first embodiment, the description thereof will be omitted. However, the heat exchanger of the third embodiment also performs heat exchange performance for each part. It can optimize and suppress the enlargement of the device.

  FIG. 4 shows the form of the heat exchanger according to the fourth embodiment of the present invention, and the basic configuration is the heat exchanger 1, 21, 31 of the first to third embodiments (see FIGS. 1 to 3). It is the same. In the heat exchanger 41 of the fourth embodiment, the number of tubes 42 of the upstream first shell 43 is the same as the number of tubes 44 of the downstream second shell 45, and each tube 42 and each tube The diameter of the tube 44 is also equal. That is, the contact area with the heating medium A per volume of the heated fluid L is not different between the pipe 42 and the pipe 44, and the liquid phase flow rate and the gas phase are also measured in the flow rate of the heated fluid L. There is no big difference over the difference of the flow velocity. However, in the first shell 43, the interval between the tubes 42 is set wider than the interval between the tubes 44 in the second shell 45, so that more heat medium A flows between the tubes 42. Yes. The area of the cross section perpendicular to the pipe 42 of the first shell 43 is larger than the area of the cross section perpendicular to the pipe 44 of the second shell 45, and the capacity of the heating medium A in the first shell 43 is larger than that of the second shell 45. Is also getting bigger.

  In this way, in the first shell 43, the capacity of the heating medium A that exchanges heat with the heated fluid L is sufficiently large with respect to the volume of the heated fluid L flowing through the pipe 42. Therefore, in the first shell 43 in which the heated fluid L is vaporized, the amount of heat exchange between the heated fluid L and the heat medium A can be increased, and the freezing of the heat medium A can be prevented.

  Since other configurations and operational effects are the same as those of the heat exchanger of the first embodiment, the description thereof will be omitted, but the heat exchanger of the fourth embodiment also performs heat exchange performance for each part. It can optimize and suppress the enlargement of the device.

  FIG. 5 shows an example of a heat exchange system to which the heat exchanger of the present invention as described above is applied. Here, a case where the same heat exchanger 1 as that of the first embodiment (see FIG. 1) is employed as the heat exchanger is illustrated.

  In this heat exchange system, heat supplied to the first shell 3 on the upstream side and the second shell 5 on the downstream side uses a configuration in which the shell of the heat exchanger 1 is divided into two stages, the upstream side and the downstream side. The flow rate of the medium A can be individually adjusted.

  The pump 10 is configured to pump seawater as the heat medium A and send it to the first shell 3 and the second shell 5 through the heat medium supply channel 11. The heat medium supply flow path 11 is branched downstream of the pump 10 into a first branch path 11 a and a second branch path 11 b, and the first branch path 11 a is connected to the heat medium inlet 3 d of the first shell 3 and the second branch path 11 a. The branch paths 11b are connected to the heat medium inlet 5d of the second shell 5, respectively. A first heat medium flow valve 12 and a second heat medium flow valve 13 are provided in the middle of the first branch path 11a and the second branch path 11b, respectively. The amount of the heating medium A fed into the shell 5 can be adjusted. The heat medium A sent to the first shell 3 and the second shell 5 from the heat medium inlets 3d and 5d is discharged from the heat medium outlet 3e or the heat medium outlet 5e, respectively. In addition, although the case where seawater was distribute | circulated as the heat medium A was illustrated here, you may employ | adopt the system which circulates heating medium, such as an antifreeze liquid, for example besides this.

  The output of the pump 10 is controlled by a flow rate control signal 10 a input from the control device 14 to the pump 10, whereby the flow rate of the heat medium A sent to the heat medium supply channel 11 is manipulated. The control device 14 is a control device that controls the entire heat exchange system using the heat exchanger 1, and the opening amounts of the first heat medium flow valve 12 and the second heat medium flow valve 13 are also indicated as opening signals. Control is performed via 12a and 13a.

  The intermediate shell 6 of the heat exchanger 1 is provided with a temperature sensor 15 and a pressure sensor 16, and the temperature sensor 15 and the pressure sensor 16 detect the temperature and pressure of the heated fluid L in the intermediate shell 6, The temperature signal 15a and the pressure signal 16a are input to the control device 14, respectively.

  The heated fluid L is supplied from the tank 17 through the heated fluid supply flow path 18 to the heated fluid inlet 8 a provided in the front chamber 8 below the heat exchanger 1. A heated fluid flow valve 19 is provided in the middle of the heated fluid supply flow path 18, and the heated fluid supplied to the heat exchanger 1 by changing the opening degree of the heated fluid flow valve 19. The amount of L can be adjusted. The opening degree of the heated fluid flow rate valve 19 is operated by an opening degree signal 19 a input from the control device 14.

  With the above configuration, in the control device 14, the supply amount of the heated fluid L to the heat exchanger 1, the first shell 3, and the second shell 2 are based on the detected values of the temperature and pressure of the heated fluid L in the intermediate shell 6. The supply amount of the heat medium A to the shell 5 can be adjusted as appropriate. Since the temperature of the heating medium A varies depending on various conditions such as the climate, the state of the heated fluid L is constantly monitored by the intermediate shell 6. For example, when the temperature of the heated fluid L is low, the pump The amount of heat medium A supplied from the second shell 5 is increased by increasing the supply amount of the heat medium A from 10 and increasing the opening of the second heat medium flow valve 13 to increase the amount of heat medium A supplied to the second shell 5. The amount of superheat of the heated fluid L is increased by increasing the exchange amount. For example, if the pressure of the fluid L to be heated in the intermediate shell 6 is low, the supply amount of the heat medium A from the pump 10 is increased and the opening degree of the first heat medium flow valve 12 is increased. The amount of the heat medium A supplied to the shell 3 is increased, the amount of heat exchange in the first shell 3 is increased, and vaporization of the heated fluid L is promoted. Alternatively, the supply amount of the heated fluid L can be increased by increasing the opening of the heated fluid flow valve 19. In addition, the control device 14 can execute various adjustments regarding the supply amount of the heated fluid L and the heating medium A depending on the detected temperature and pressure of the heated fluid L. In addition, although the case where the temperature sensor 15 and the pressure sensor 16 are provided as sensors for monitoring the state of the fluid L to be heated is illustrated here, only one of the temperature sensor 15 and the pressure sensor 16 is provided. It is possible to control the supply amount of the heated fluid L and the heating medium A.

  At this time, in the heat exchange system of the present embodiment, the supply of the heat medium A to the first shell 3 where the heated fluid L is mainly vaporized and the second shell 5 where the heated fluid L is overheated. Since the supply of the heating medium A is controlled separately, the vaporization amount and the superheat amount can be individually operated. Therefore, an operation for maintaining the amount and temperature of the heated fluid L finally discharged from the heated fluid outlet 9a in a required state is easy.

  Moreover, in grasping the state of the fluid L to be heated in the heat exchanger 1, the installation location of the temperature sensor 15 and the pressure sensor 16 is intermediate between the first shell 3 where vaporization is performed and the second shell 5 where overheating is performed. The intermediate shell 6 corresponding to the point is used. Since the state of the heated fluid L is monitored at a point on the way from vaporization to overheating, for example, compared with the case where the temperature sensor 15 and the pressure sensor 16 are attached to the front chamber 8 and the rear chamber 9, for example, It is possible to appropriately grasp the heating status of the heating fluid L.

  As described above, since the heat exchange system of the present embodiment includes at least one of the temperature sensor 15 or the pressure sensor 16 in the heat exchanger 1, the vaporization amount of the fluid L to be heated by the heat exchanger 1 The amount of superheat can be individually operated, and the operation can be facilitated in maintaining the amount and temperature of the heated fluid L finally discharged in a required state.

  In the heat exchange system of the present invention, since the temperature sensor 15 or the pressure sensor 16 is provided in the intermediate shell 6, it is possible to appropriately grasp the heating status of the heated fluid L in the heat exchanger 1. .

  Other configurations and operational effects are the same as the operational effects of the heat exchanger of the first embodiment employed in the system, and thus the description thereof will be omitted. However, according to the heat exchange system of the present embodiment, The performance related to the heat exchange can be optimized for each part, and the size of the apparatus can be suppressed.

  The heat exchanger and heat exchange system of the present invention are not limited to the above-described embodiments, and various fluids other than LNG can be assumed as the fluid to be heated. Of course, various changes can be made without departing from the scope of the invention.

1 Heat exchanger 2 First heating line (pipe)
3 First shell 4 Second heating line (pipe)
5 Second shell 6 Intermediate shell 15 Temperature sensor 16 Pressure sensor 21 Heat exchanger 22 First heating line (pipe)
23 1st shell 24 2nd heating line (pipe)
25 Second shell 31 Heat exchanger 32 First heating line (pipe)
33 First shell 34 Second heating line (pipe)
35 Second shell 41 Heat exchanger 42 First heating line (pipe)
43 First shell 44 Second heating line (pipe)
45 Second shell A Heating medium L Heated fluid

Claims (6)

A first shell configured to house a first heating line through which a fluid to be heated is circulated, and to supply a heat medium around the first heating line;
A second shell configured to house a second heating line for circulating the fluid to be heated that has passed through the first heating line, and to supply a heating medium around the second heating line;
An intermediate shell located between the first shell and the second shell, and configured to circulate a fluid to be heated in a space provided therein;
At least one of the flow path cross-sectional area of the heated fluid in the first shell, the contact area with the heating medium per volume of the heated fluid, or the capacity of the heating medium per volume of the heated fluid is the second A heat exchanger configured to be larger than the shell.   The first heating line is configured as a plurality of tubes, the second heating line is configured as one or more tubes, and the number of tubes constituting the first heating line constitutes the second heating line. The heat exchanger according to claim 1, wherein the number is greater than   The first heating line and the second heating line are each configured as a plurality of tubes, and the interval between the tubes constituting the first heating line is set wider than the interval between the tubes constituting the second heating line. The heat exchanger according to claim 1, wherein an area of a cross section perpendicular to the tube of the first shell is set larger than an area of a cross section orthogonal to the tube of the second shell.   The heated fluid introduced into the first heating line from the lower part of the first shell is configured to be extracted to the upper side of the second heating line through the intermediate shell. The heat exchanger as described in.   The heat exchange system using the heat exchanger according to claim 1, wherein the heat exchanger includes at least one of a temperature sensor that detects a temperature of the heated fluid and a pressure sensor that detects a pressure of the heated fluid.   The heat exchange system according to claim 5, wherein the temperature sensor or the pressure sensor is provided in the intermediate shell.

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